CN101896581B - Process and plant for producing char and fuel gas - Google Patents

Process and plant for producing char and fuel gas Download PDF

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Publication number
CN101896581B
CN101896581B CN200780101881.4A CN200780101881A CN101896581B CN 101896581 B CN101896581 B CN 101896581B CN 200780101881 A CN200780101881 A CN 200780101881A CN 101896581 B CN101896581 B CN 101896581B
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fluidized
bed reactor
gas
oxygen
coke
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CN101896581A (en
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A·奥斯
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Metso Minerals Ltd
Outotec Finland Oy
Metso Finland Oy
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Outokumpu Technology Oyj
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
    • C10B49/08—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form
    • C10B49/10—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form according to the "fluidised bed" technique
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/463—Gasification of granular or pulverulent flues in suspension in stationary fluidised beds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/62—Processes with separate withdrawal of the distillation products
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B11/00—Making pig-iron other than in blast furnaces
    • C21B11/10—Making pig-iron other than in blast furnaces in electric furnaces
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/0006—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state
    • C21B13/0013—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state introduction of iron oxide into a bath of molten iron containing a carbon reductant
    • C21B13/002—Reduction of iron ores by passing through a heated column of carbon
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/0066—Preliminary conditioning of the solid carbonaceous reductant
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/0073—Selection or treatment of the reducing gases
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/08—Making spongy iron or liquid steel, by direct processes in rotary furnaces
    • C21B13/085—Making spongy iron or liquid steel, by direct processes in rotary furnaces wherein iron or steel is obtained in a molten state
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903—Feed preparation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903—Feed preparation
    • C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903—Feed preparation
    • C10J2300/0909—Drying
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1838—Autothermal gasification by injection of oxygen or steam
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
    • C21B2100/20—Increasing the gas reduction potential of recycled exhaust gases
    • C21B2100/22—Increasing the gas reduction potential of recycled exhaust gases by reforming
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
    • C21B2100/40—Gas purification of exhaust gases to be recirculated or used in other metallurgical processes
    • C21B2100/44—Removing particles, e.g. by scrubbing, dedusting
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/10—Reduction of greenhouse gas [GHG] emissions
    • Y02P10/134—Reduction of greenhouse gas [GHG] emissions by avoiding CO2, e.g. using hydrogen

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Manufacturing & Machinery (AREA)
  • Metallurgy (AREA)
  • Combustion & Propulsion (AREA)
  • Dispersion Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)

Abstract

The present invention relates to a process and a plant for producing char and fuel gas. In a fluidized bed reactor (1) carbonaceous material like coal is degasified with oxygen containing gasses in the presence of steam. More than 60 % of the fixed carbon in the carbonaceous material is recovered in the produced char.

Description

Produce the method and apparatus of coke and fuel gas
Technical field
The present invention relates to a kind of method of coke and fuel gas and device accordingly produced, wherein in the temperature higher than approximately 1000 ℃ and extremely with oxygen-containing gas, the carbonaceous material of for example coal is degassed in the situation that there is steam in the fluidized-bed reactor with circulating fluidized bed under the pressure of approximately 40 bar at approximately 1 bar.
Known a kind of for produce the method and apparatus of fuel gas and process heat from carbonaceous material from EP 0 062 363 A1.In the method, coal or analogue react with oxygen-containing gas in fluidized-bed reactor in the situation that there is steam.At the pressure up to 5 bar with carry out degassed at the temperature of 800 ℃ to 1100 ℃.For the fuel that makes to obtain from the method and hot amount maximize, by the parameter adjustment of fluidized-bed reactor, be that the carbon in 40% to 80% initial feed is reacted in fluidized-bed reactor.Similarly method sees US4, and 474,583 and JP 2003105351.
The many metallurgical technologies that are similar to the melting and reducing of the iron ore in fusion reducing furnace (H1smelt-SRV) or the reduction of the ilmenite in rotary kiln need to be such as coke powder, coke, the carbonaceous material of hard coal or power plant's coal.Yet, produce the fuel of maximum and the known method of heat and be unsuitable for obtaining the enough coke using or analogue in this type of metallurgical technology.In addition, the coke of preferred low volatile content, because this can cause saving the energy and increase the output in metallurgical technology.
Invention is described
Therefore, the object of the present invention is to provide the method and apparatus of producing coke and fuel gas for optimizing the use of carbon, think that coking provides necessary heat and thereby when generating fuel gas, produces the coke of maximum.
According to the present invention, this object is solved by a kind of method, the method is characterized in that, the oxygen supply in reactor is regulated or is adjusted into the fixed carbon over 60% making in carbonaceous material and be recycled in produced coke.Therefore, the present invention be take and only with minimum carbon, as coking provides the mode of necessary heat, integrated the production of hot coke and fuel gas.Therefore, produced the fuel gas of high calorie,, most carbon has been recovered in the solid product that can be used for further metallurgical technology meanwhile.Coke according to the present invention is carbonaceous material, and it is heat-treated and mainly contains carbon and ash, and having some remaining a small amount of contents is mainly hydrogen and oxygen.
According to a preferred embodiment of the invention, oxygen supply in reactor is regulated or is adjusted into the lower region of reactor or the oxygen availability of bottom zone are compared still less with the upper zone of reactor.Preferably oxygen supply in reactor is regulated or is adjusted into the upper zone that makes the lower region of reactor or the oxygen availability of bottom zone be less than reactor oxygen availability 50%, be preferably less than 80%.For example, the oxygen availability of the lower region of reactor or bottom zone can be less than reactor upper zone oxygen availability 90%.By doing like this, will on this reactor theory, be divided into two sections.The oxygen free gas supply of hypomere is low, thereby the less fixed carbon that burnt, and causes particularly when expectation coarse particles product, having higher carbon yield.
Most of energy of the method is to provide on the top of reactor, there, volatile matter and duff grain and oxygen such as injecting are still very high thereby have the district of good heat transmission to burn at granule density, avoided particle agglomeration, and this is easy in the reactor assembly being diluted as the combustion zone of bubbling fluidized bed occur.In addition, good heat transmission has been guaranteed in the circulation of the particle in reactor, and this is also crucial in the free plate of dilution routine, fixed fluidized bed or fixed-bed reactor.
Because volatile matter is not in any case that fixed carbon and fine particle all can run off with degassed logistics, so the yield of not remarkably influenced of the carbon unit fixed carbon of burning.Yet, by reactor being separated and being made a region be devoted to generate energy, even in more than 1000 ℃ high temperature ranges, also can in fluidized-bed reactor, realize high fixed carbon yield (> 60%), avoided the generation of a large amount of tar.
By use using oxygen content be less than bottom that 5% gas or air be fed to reactor and/or bottom as fluidizing agent and using oxygen content be 50% to approximately 100%, preferably between 90% and 99%, particularly there is the oxygen rich gas of the oxygen content that is at least 95% or top that oxygen-rich air is fed to fluidized-bed reactor as the circulating fluidized bed (CFB) of secondary air (secondary gas), can in product, realize and be greater than 60%, be preferably greater than 70% fixed carbon yield.
According to a preferred embodiment of the invention, the temperature of reaction in the circulating fluidized bed of fluidized-bed reactor is between approximately 1000 ℃ and approximately 1100 ℃.Although temperature can be between 950 ℃ to 1150 ℃ particularly between 980 ℃ and 1100 ℃, preferably higher than the temperature of reaction of 1000 ℃, preferably higher than 1050 ℃.Reaction pressure in the method for the invention can be between 1 bar and 40 bar, preferably between 1.1 bar and 30 bar.Yet the pressure in preferred streams fluidized bed reactor is higher than approximately 5 bar and lower than 20 bar.
In addition steam and the mixture of gas or air or the mixture of these gases are fed in the circulating fluidized bed of fluidized-bed reactor as mainstreaming gas, or as to substituting above.In addition, also can use recycle gas.Can adjust the content of quantity and ratio and their oxygen and other component of feed gas.
Method of the present invention is adjusted into coke removal and also generates the fuel gas of high calorie outward.By the degassed fuel gas producing of carbonaceous material preferably being had to 9MJ/m in fluidized-bed reactor 3(STP) minimum calorific value.This fuel gas preferably has low tar content.
In order to ensure reuse heat energy and fuel gas in method of the present invention, a closed circuit gas flow system can be provided, and the tail gas of fluidized-bed reactor is fed to waste heat boiler and is incorporated in fluidized-bed reactor to produce steam and to be used as at least partly fluidizing agent.This quantity can control and adjust.The gas that leaves waste heat boiler can be in multiclone or for example part dedusting in the dust-removal system of any other type of fabric or metal or porcelain filter or electrostatic precipitator, and before fuel gas is reintroduced back to fluidized-bed reactor, supplies with that process gas washing unit carries out further purifying and cooling.In addition, the content of recycle gas can be by adding or removing such as the component of water, carbonic acid gas, oxygen, pollutent and/or impurity and control.Before using fuel gas or recycle gas, also can for example lead to that heat transfer or partial combustion reheat this gas and use procedure energy reheats.
Advantageously, by the solid instant heating coke producing in fluidized-bed reactor higher than approximately 750 ℃, preferably at the temperature between 950 ℃ and 1100 ℃, transfer in the device such as smelting furnace or rotary kiln.The heat energy of the hot coke therefore, producing in fluidized-bed reactor can recycle in other metallurgical technology.
In another preferred embodiment of the present invention, by pneumatic injection and/or haulage system, the hot coke producing is sent to the device for the metallurgical technology of the melting and reducing such as iron or ilmenite reduction.Or hot coke is not directly sent to Metallurgical Factory, and can be collected in middle warehouse, it is fed in melting reactor or reduction reactor or analogue therefrom.Therefore the coke, producing can be piled up or fill out to be stored in sealing storage carriage and transport.Also can be using coke for any other non-metallurgical technology that technique such as electricity as sintering, pelletizing, metal refines thing as a supplement and produces for for example power station or element phosphor easily.
Preferably the wet coal as carbon-containing feeding is predrying and be crushed to the granular size below 10 millimeters, then this coal is sent in fluidized-bed reactor.With haulage system, will wet coal from accumulation confession dewing coal bunker.Wet coal bunker can be useful on the storage capacity of operation in 15 hours.By the coal pulverizer of receiving simultaneously dry to remove surface-moisture, preferably fast as far as possible.Afterwards, coal can be stored in the storehouse for dry coal, and/or is continued to be transferred in fluidized-bed reactor by pneumatic conveying and dosing system.Therefore can use moisture content to reduce to lower than 5% carbon-containing feeding hard coal and steam coal and/or surface-moisture content and reduce to brown coal and the brown coal lower than 17%.The water-content of pre-dried coal can need to control according to required technique.From the effluent gas in the drying process of coal, can from other gas, remove, and can for example according to AU 2,005 237 179, in special device, process, or in this technique, reuse, for example after heating as the vapoury gas on the top of injecting reactor or as the part of fluidizing agent and/or recycle gas.Pre-dried coal can be heated and can remove between this heating period a part for volatile matter.This gas stream also can individual curing, for example, as process gas or for burning.
In order to use, preferably use the coke of low volatile content, because this can cause energy-conservation and increase output in metallurgical technology.Therefore, according to a preferred embodiment of the invention, the volatile content of the coke producing in fluidized-bed reactor is lower than 10wt%, preferably lower than 4wt%.
According to device of the present invention, method that be specially adapted to carry out above-mentioned production coke and fuel gas, comprise: preferably with the fluidized-bed reactor of circulating fluidized bed or with internal recycling as the annular fluidized bed reactor of DE102 60 734, for another reactor of another metallurgical technology, and the pneumatic injection and/or the haulage system that between described fluidized-bed reactor and described another reactor, provide.Described fluidized-bed reactor is furnished with: the entrance for mainstreaming gas providing in this reactor compare Di district and be connected with the supply of steam and the mixture of gas or air or these gases, above-mentioned for the entrance of mainstreaming gas above and the secondary air entrance that is connected with the supply of the mixture of oxygen rich gas or oxygen-rich air or these gases, with coal dry and that pulverize or solid inlet that similarly supply of carbonaceous material is connected.According to the present invention, mainstreaming gas inlet is connected with the first gas or air supply, secondary air entrance is connected with the second oxygen rich gas or oxygen-rich air supply, and the oxygen content of the first gas or air supply is fewer than the oxygen content of the second oxygen rich gas or oxygen-rich air supply.This free oxygen of lower region of having guaranteed reactor is few, thereby burns less fixed carbon, causes particularly when expectation coarse particles product, having higher carbon yield.In this case, most of energy of the method is to provide on the top of reactor, and there, volatile matter and duff grain and oxygen such as injecting are still very high thereby have the district of good heat transmission to burn at granule density, have avoided the reunion of particle.Should point out, according to the present invention, described device can be configured to the coke that makes to produce in fluidized-bed reactor and can pile up or fill out and be stored in sealing storage carriage transportation rather than hot coke is imported into another reactor for other metallurgical technology or imports hot coke into another reactor for other metallurgical technology afterwards.
In a preferred embodiment of the invention, in the downstream of fluidized-bed reactor, provide cyclonic separator and/or multiclone, for coke and dust and fuel gas are separated, the outlet of cyclonic separator and/or multiclone is connected with pipeline, usings the fuel gas of charging is fed in fluidized-bed reactor and/or fed in the fluidized bed cooler providing in the downstream of fluidized-bed reactor as fluidizing agent.Or, can use any other dust-removal system of fabric for example or porcelain filter or electrostatic precipitator.Therefore, can provide closed circuit gas flow system to come recirculation and the process gas that produces of recycling at least a portion for fluidisation.
Advantageously coke is sent to another reactor for other process, is preferred for the reactor of metallurgical process, such as be smelting furnace for the melting and reducing of iron, for the rotary kiln of ilmenite reduction or the electric furnace that refines for the electricity of metal.Before coke is sent to another reactor, coke can be cooled and/or with fluidized-bed reactor in mix dust.
It is that solid cooled is combined with the preheating of oiler feed and is sent to the device height of expectation simultaneously that another of cooling coke product preferably selected.For this reason, preferably use the method that annular fluidized bed reactor assembly is combined with vertical pneumatic transport reactor as DE 102 60 738.Preferably the economizer that in the annulus wheel of cooling bundle insertion fluidized-bed is the waste heat boiler in waste gas train is conducted heat.
Apply progress of the present invention, advantage and possibility also can and draw from the explanation of embodiment below from accompanying drawing.All explanations and/or illustrated feature self or its combining form have formed theme of the present invention, and list in claim or their reference background document irrelevant with them.
Accompanying drawing summary
Fig. 1 shows according to the artwork of the method and apparatus of the first embodiment of the present invention.
Fig. 2 shows according to the artwork of the method and apparatus of the second embodiment of the present invention.
Detailed description of preferred embodiments
Device shown in Fig. 1 comprises: fluidized-bed reactor 1, and it has circulating fluidized bed; Cyclonic separator 2, it is provided at the downstream of circulating fluid bed reactor 1 (CFB reactor).The first entrance 3 for introducing mainstreaming gas is provided in fluidized-bed reactor 1, for introducing the second entrance 4 of secondary air and for introducing the 3rd entrance 5 of solid.The first entrance 3 is connected to the supply of the mixture of steam and gas or air or these gases.The second entrance 4 is connected to the supply of the mixture of oxygen rich gas or oxygen-rich air or these gases.Therefore, by the second entrance 4, the oxygen availability in the upper zone of oxygen rich gas or oxygen-rich air introducing reactor 1 is wherein compared obviously higher with the lower region of the reactor 1 at the first entrance 3 places.The 3rd entrance 5 can be a part for pneumatic conveying system (not shown in Fig. 1), so that dry coal or similar carbonaceous material are fed to fluidized-bed reactor 1.Or coal can be used lock hopper and machinery and volume delivery system for example rotary valve or worm conveyor introducing CFB reactor.
Can provide storage area in the upstream of fluidized-bed reactor 1, with haulage system, coal is supplied to the wet coal bunker of the storage capacity that can have operation in 15 hours from this storage area.In addition, can provide coal pulverizer and dehumidification system, therein the coal dust of receiving is broken into 10 millimeters of following granular sizes simultaneously dry to remove as much as possible surface-moisture.Before in coal being sent into fluidized-bed reactor 1 continuously by pneumatic conveying and dosing system, coal can be stored in dry coal storehouse.
In order to realize the uniform gas speed on the whole height of circulating fluid bed reactor 1, in bottom zone, (not shown in Fig. 1) is shaped to taper by the cross section of reactor.As shown in Figure 2, can using recycle gas as fluidizing agent, introduce in the method by nozzle grid.Because gas velocity is high, on the whole height of fluidized-bed reactor 1, solid is all carried secretly, makes suspended solids among continuous motion.Solid or leave reactor and reclaim (outer circulation) by cyclonic separator 2 with air-flow, or flow back on reactor wall again to become entrained in (internal recycle) in fluidizing agent at reactor bottom.This strong solid/gas mixing behavior is the feature with the system of circulating fluidized bed, and has guaranteed fabulous heat transfer and mass transfer and the almost uniform temperature distribution in whole fluidized-bed reactor 1.
The fuel gas producing in fluidized-bed reactor 1 and entrained solid thereof are discharged into cyclonic separator 2 so that coke and dust and the fuel gas that can discharge by pipeline 6 are separated.The major portion of the particle of carrying secretly in leaving the gas of fluidized-bed reactor 1 is separated with process gas in reclaiming cyclonic separator 2, and turns back to circulating fluidized bed by pipeline 7, by sealed can, forms external circulation.From the material of sealed can and the material that comes from the bottom of fluidized-bed reactor 1 by pipeline 7a by water-cooled disposal facilities so that keep the speed of constant pressure reduction to discharge at the height of reactor, this is reactor stock's measure.
Solids such as coke and dust that discharge from cyclonic separator 2 by pipeline 7 or that discharge from the outlet of fluidized-bed reactor 1 by pipeline 7a can be fed to another reactor 8, for example, for the smelting furnace of the melting and reducing of iron or for the rotary kiln of ilmenite reduction.Can be by hot coke and analogue being transferred in reactor 8 from pipeline 7 with the pneumatic injection shown in arrow and haulage system 9 in Fig. 1.
See now Fig. 2, as mentioned above, described device is furnished with fluidized-bed reactor 1 and cyclonic separator 2.
Likely in 1 upstream of fluidized-bed reactor, provide wet coal storage warehouse, coal pulverizer and dehumidification system, dry coal storage warehouse and/or for the pneumatic conveying (not illustrated in FIG.) of dry coal.
By pipeline 7, from hot coke cyclonic separator 2 discharges and/or that discharge from fluidized-bed reactor 1, be supplied to fluidized bed cooler 10.This coke may be supplied with subsequently and pass on container 11 and/or by being that injection and the haulage system 9 of hot delivery system is sent to another reactor 8.
Fluidized bed cooler 10 is the moderate fluidisations that realize low gas velocity, only enough maintains solids movement and allows large or fine granule to mix.By injected water or for example, by other means (cooling bundle), control temperature, the outlet temperature of material is adjusted into the highest delivery temperature of processing 850 ℃.The tail gas (fuel gas) that leaves fluidized bed cooler 10 can be injected in process gas washer process gas system before.Suppose that volatile content is lower than 3wt% in the coke of discharge.
By pipeline 6, leave the fuel gas of cyclonic separator 2 and introduce waste heat boiler 12 at approximately 1000 ℃, the steam in waste heat boiler 12 feeds water to produce by heating boiler.After cooling in waste heat boiler 12, dedusting at least partly in the multiclone 13 that fuel gas provides in the downstream at waste heat boiler 12.From multiclone 13, the dust of discharge can mix with the coke of discharging from circulating fluidized bed, and is transferred to fluidized bed cooler 10 or passes in container 11.
The fuel gas that leaves multiclone 13 at approximately 400 ℃ may further be purified and/or be cooled to approximately 30 ℃ in process gas scrubber unit (not shown).The energy of the fuel gas producing can be used for for example predrying and/or preheat carbonaceous material and/or preheat other technique material.In settler, process the process water from washer, produce the mud of rich carbon.The overflow of settler is recycled to washer.The mud of rich carbon can be recycled in coal pulverizer and drying plant, or is directly being recycled in technique stove after for example reuniting or compressing.
In closed circuit gas flow system, then can purification and cooling fuel gas be discharged by pipeline 14, or be reintroduced back at least in part in described technique by pipeline 15.This quantity can control and/or adjust.As shown in Figure 2, fuel gas can be used as fluidizing agent and sends in fluidized bed cooler 10 and/or can be used as fluidizing agent and send in fluidized-bed reactor 1.Before using fuel gas or recycle gas, the content of gas can be by adding or removing and control and/or adjust as the component of steam, carbonic acid gas or hydrogen sulfide.
This device can operate under normal pressure situation or preferably under the pressure higher than 5 bar.Yet due to the pressure-losses and material load, the pressure producing can be higher.Therefore, may provide the recycle gas compressors of recompression flow of process gas to carry out the pressure-losses of compensation system.Process water and mechanical water coolant cooling and recycled back in cooling tower.
Embodiment 1 (producing coke and fuel gas)
In the device shown in Fig. 2, with the wet subbituminous coal of 385 tons/hour, as carbonaceous material, produce coke and fuel gas, this subbituminous coal is pulverized and is dried that moisture content is reduced to 14wt%, then by entrance 5, sends in the circulating fluidized bed of fluidized-bed reactor 1.The C of the coal of sending into composed as follows: 77wt% (daf=is dry and ashless); The H of 4.1wt% (daf); The O of 16.91wt% (daf); The S of 0.65wt% (daf); The N of 1.34wt% (daf) and the ash of 9.1wt%.Volatile content is 35.3wt% (d.b.=butt), and fixed carbon content is 55.6wt% (d.b.).
Be used as secondary air to pass through entrance 4 and feed 62 of reactor, 000Nm 3low-pressure steam (900kPag) gentleization of partial combustion coal in circulating fluidized bed of the oxygen of/h (95% oxygen) and 5 tons/hour.Reactor use by entrance 3, introduce 90,000m 3the recycle gas of/h (STP) carrys out fluidisation, and described recycle gas has 39.3% carbon monoxide, 13.1% carbonic acid gas, 37.6% nitrogen, 1.4% water, 2.4% methane, 0.4% hydrogen sulfide and 5.8% nitrogen.Temperature in circulating fluidized bed is higher than 1000 ℃, and pressure is 500kPag.
The partial combustion of carbon and gasification are undertaken by following reaction:
2C+11/2O 2＝CO+CO 2
C+H 2O＝CO+H 2
Suppose to leave the CO/CO of the process gas of circulating fluid bed reactor 1 2ratio be 2.90.Produced 274,000m 3/ h (STP) fuel gas, it is composed as follows: the carbonic acid gas of 12.7 volume %; The nitrogen of 6.0 volume %; The oxygen of 0 volume %; The carbon monoxide of 40.1 volume %; The hydrogen of 38.6 volume %; The methane of 2.5 volume %; The water of 0.1 volume %; The hydrogen sulfide of 50ppmv.
In addition, produced the coke of 152 tons/hour, its carbon content is that 80wt% and volatile matter (residual ash) are 2wt%.This solid product being comprised of carbon and ash can be discharged by the exhausting line after reclaiming cyclonic separator 2, or discharges from the bottom of fluidized-bed reactor 1.What produce is meticulous so that can not discharge at multiclone 13 at the dust that reclaims cyclonic separator 2 discharges, from the coke of fluidized-bed reactor 1 with from the dust of multiclone 13, in fluidized-bed reactor 10, mix, this fluidized-bed reactor 10 is also for being cooled to product the temperature lower than 850 ℃.Or multiclone dust stream can merge with the cooled product from fluidized bed cooler 10.
The cold recycle gas of fluidized-bed reactor 10 use carrys out fluidisation and cooling.In addition, if suitable, water can be injected in fluidized-bed reactor 10 with further cooling.Or, also can use indirect cooler.
From the product of fluidized-bed reactor 10, be transported to transfer container 11, use hot delivery system that it is delivered to another reactor 8, for example smelt reduction vessel therefrom.Or this product can be piled up or fill out to be stored in sealing storage carriage and transport.
The fuel gas leaving at the cyclonic separator 2 in the downstream of fluidized-bed reactor 1 is cooled to temperature lower than 450 ℃ in waste heat boiler 12, then makes this fuel gas enter multiclone 13.The ultrafine powder that always can not be discharged from multiclone can be used as mud and is discharged by Venturi type laveur (not shown).Then mud can be transported to settler.Suppose to have the coke producing of 10wt% be used as mud and collect.In an integrating device, this mud can be dried by the coal of the upstream at fluidized-bed reactor 1 and pulverizing unit (not shown) carries out recirculation.
In addition, the process gas of being discharged by multiclone 13 (fuel gas) can be further cooling in process gas water cooler (not shown), and can be delivered to subsequently battery limit (BL) (not shown) and further use.Part process gas is by pipeline 15 recirculation and as the circulating fluidized bed of fluidized-bed reactor 1 and the fluidizing agent of fluidized bed cooler 10.In addition, the process gas of a tittle is used as to fuel gas with moisture-free coal.
Reference numeral:
1 circulating fluid bed reactor
2 cyclonic separators
3 first entrances (gas)
4 second entrances (gas)
5 the 3rd entrances (solid)
6 pipelines
7,7a pipeline
8 another reactors
9 spray and haulage system
10 fluidized bed coolers
11 containers
12 waste heat boilers
13 multiclones
14 pipelines
15 pipelines

Claims (15)

1. a method of producing coke and fuel gas, wherein in the temperature higher than 1000 ℃ and with oxygen-containing gas, carbonaceous material is degassed in fluidized-bed reactor (1) under the pressure of 1 bar to 40 bar, wherein the oxygen supply in described fluidized-bed reactor (1) being regulated or is adjusted into the fixed carbon over 60% making in carbonaceous material is recycled in produced coke, it is characterized in that, oxygen supply in described fluidized-bed reactor (1) is regulated or is adjusted into the upper zone that makes the lower region of fluidized-bed reactor (1) or the oxygen availability of bottom zone be less than fluidized-bed reactor (1) oxygen availability 80%, wherein oxygen content is less than to 5% gas and is fed to the bottom of fluidized-bed reactor (1) and/or bottom as fluidizing agent, and the top that the oxygen rich gas that is 50% to 100% using oxygen content is fed to described fluidized-bed reactor (1) is as secondary air.
2. according to the method for claim 1, it is characterized in that, oxygen supply in fluidized-bed reactor (1) is regulated or is adjusted into the upper zone that makes the lower region of fluidized-bed reactor (1) or the oxygen availability of bottom zone be less than fluidized-bed reactor (1) oxygen availability 50%.
3. according to the method for claim 1, it is characterized in that, the oxygen rich gas using oxygen content between 90% and 99% is fed to the top of described fluidized-bed reactor (1) as secondary air.
4. according to the method for claim 1, it is characterized in that, the temperature of reaction in fluidized-bed reactor (1) is higher than 1000 ℃ to 1100 ℃.
5. according to the method for claim 1, it is characterized in that, the reaction pressure in fluidized-bed reactor (1) is higher than 5 bar.
6. according to the method for claim 1, it is characterized in that, the mixture of steam and gas is fed in fluidized-bed reactor (1) as mainstreaming gas.
7. according to the method for claim 1, it is characterized in that, by fluidized-bed reactor (1), by carbonaceous material, degassed being created under standard temperature and pressure (STP) has 9MJ/Nm 3the most low-calorie fuel gas.
8. according to the method for claim 1, it is characterized in that, the fuel gas recirculation that at least a portion is generated is also used as the fluidizing agent in fluidized-bed reactor (1) again.
9. according to the method for claim 1, it is characterized in that, at the temperature higher than 750 ℃, produced coke is transferred in smelting furnace or rotary kiln.
10. according to the method for claim 1, it is characterized in that, by pneumatic injection and/or haulage system (9), produced hot coke is passed to the device (8) for metallurgical technology.
11. claims 1 or 3 method, wherein said oxygen rich gas is oxygen-rich air.
12. claims 1 or 6 method, wherein said gas is air.
13. according to the method for claim 10, it is characterized in that, described metallurgical technology is that the melting and reducing of iron is, the reduction of the refinement of the electricity of metal or ilmenite.
14. according to the method for claim 1, it is characterized in that, produced coke is transported to desired device height and with heat energy, carrys out preboiler feedwater and carry out cooling simultaneously.
15. according to the method for claim 1, it is characterized in that, the volatile content of the coke producing in fluidized-bed reactor (1) is lower than 10wt%.
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